An apparatus for synthesizing acid anhydride using a microchannel reactor

Abstract

The utility model relates to the field of anhydride synthesis discloses an anhydride synthesis device using micro -channel reactor, including storage jar, the storage jar places in the top surface of bearing base, the top surface of bearing base is fixed with first metering pump, the storage jar is connected with the input end of first metering pump through the connecting pipe, the top surface of bearing base places and has the heat preservation jar, the top surface of bearing base is fixed with second metering pump, the heat preservation jar is connected with the input end of second metering pump through the connecting pipe, the top surface of bearing base is fixed with a plurality of micro -reactor body. In the utility model, through the synergies of storage jar, first metering pump, heat preservation jar, second metering pump, micro -reactor body, pressure -stabilizing jar, flash tank and tubular condenser, realized raw material accurate delivery, micro -scale reaction intensification, pressure steady state regulation and control, flash separation and condensation recovery integration process, realized the directional optimization recovery and multistage depth purification of hydrogenation product.

Description

Technical Field

[0001] This utility model relates to the technical field of acid anhydride synthesis, specifically to an acid anhydride synthesis device using a microchannel reactor. Background Technology

[0002] An acid anhydride is the residue remaining after an oxyacid loses one or more water molecules. Generally, an inorganic acid is formed by the direct loss of a water molecule from one molecule of the acid; the oxidation state of the element determining its acidity remains unchanged in the anhydride. Organic acids, on the other hand, are formed by the dehydration reaction between two or more molecules of the acid. Only oxyacids have anhydrides. Acids without oxyacids do not have anhydrides. Anhydrides can generally be considered oxides formed by the dehydration of acids (the anhydrides of organic acids are not oxides). Many acids can react with water again to return to their original form. Based on their properties, acids can be classified into anhydrides of inorganic acids and anhydrides of organic acids.

[0003] Hydrogenation reactors are a very important piece of equipment in organic chemistry laboratories and actual production processes. They can be used not only as containers for hydrogenation reactions, but also in situations where liquids and gases need to be thoroughly mixed.

[0004] Continuous hydrogenation uses homogeneous catalysts. Traditional post-treatment requires catalyst recovery through extraction, crystallization, and other methods, which leads to the following drawbacks: after the catalyst enters the separation stage with the product, it is easily discharged with waste liquid or lost with by-products. There is a lack of targeted recovery and recycling, which can easily increase catalyst consumption and production costs, while also increasing environmental protection pressure. Summary of the Invention

[0005] The purpose of this invention is to provide an acid anhydride synthesis device using a microchannel reactor to solve the problem that after the catalyst enters the separation stage with the product, it is easily discharged with waste liquid or lost with by-products, lacking targeted recovery and recycling, which easily increases catalyst consumption and production costs, and at the same time increases environmental treatment pressure.

[0006] To achieve the above-mentioned utility model objectives, the present utility model adopts the following technical solution: an acid anhydride synthesis device using a microchannel reactor, comprising a storage tank placed on the top surface of a load-bearing base, a first metering pump fixed on the top surface of the load-bearing base, the storage tank being connected to the input end of the first metering pump via a connecting pipe, a heat preservation tank placed on the top surface of the load-bearing base, a second metering pump fixed on the top surface of the load-bearing base, the heat preservation tank being connected to the input end of the second metering pump via a connecting pipe, several microreactor bodies fixed on the top surface of the load-bearing base, a pressure stabilizing tank placed on the top surface of the load-bearing base, the pressure stabilizing tank being connected to the microreactor body via a connecting pipe, a flash evaporator placed on the top surface of the load-bearing base, the flash evaporator being connected to the pressure stabilizing tank via a connecting pipe, a pipe-type condenser fixed on the top surface of the load-bearing base, the pipe-type condenser being connected to the flash evaporator via a connecting pipe, and a discharge pipe fixedly connected to both the pipe-type condenser and the flash evaporator.

[0007] Preferably, a mounting base is fixed to the front side of the load-bearing base, a mounting frame is fixed to the top surface of the mounting base, a fixed base is fixed to the right side of the mounting base, a first buffer tank is placed on the top surface of the fixed base, two feed pipes are connected and fixed to the first buffer tank, a high-pressure diaphragm pump is connected to the mounting frame by screws, a pipeline explosion-proof preheater is connected to the mounting frame by screws, the output end of the high-pressure diaphragm pump is connected to the input end of the pipeline explosion-proof preheater through a connecting pipe, a hydrogenation reactor is connected to the mounting frame by screws, and the first buffer tank is connected to the input end of the hydrogenation reactor through a connecting pipe. The output end of the device is connected to the input end of the hydrogenation reactor via a connecting pipe. A coil-type condenser is placed on the top surface of the fixed base. The input end of the coil-type condenser is connected to the output end of the hydrogenation reactor via a connecting pipe. A gas-liquid separator is placed on the top surface of the fixed base. The gas-liquid separator is connected to the output end of the coil-type condenser via a connecting pipe. A second buffer tank is placed on the top surface of the fixed base. The gas outlet of the second buffer tank is connected to the input end of the gas-liquid separator via a connecting pipe. The output ends of the gas-liquid separator and the second buffer tank are connected via a three-way pipe. A regulating valve is fixed on the three-way pipe. The three-way pipe is connected to a storage tank.

[0008] Preferably, a back pressure valve is fixed on the connecting pipe at the outlet end of the second buffer tank.

[0009] Preferably, a first flow meter and a second flow meter are fixed on the two feed pipes of the first buffer tank, respectively. The first flow meter is an H2 mass flow meter, and the second flow meter is an N2 mass flow meter.

[0010] Preferably, the number of microreactor bodies is three, and the three microreactor bodies are connected in series through connecting pipes. The microreactor bodies are arranged from front to back as: a primary microreactor body, a secondary microreactor body, and a tertiary microreactor body.

[0011] Preferably, an explosion-proof electrical cabinet is fixed to the top surface of the mounting base, an explosion-proof touch screen is fixed to the explosion-proof electrical cabinet, an alarm light is fixed to the top surface of the explosion-proof electrical cabinet, an emergency switch is provided on the explosion-proof electrical cabinet, and the explosion-proof electrical cabinet, the alarm light, and the emergency switch are electrically connected.

[0012] Compared with the prior art, the present invention has the following beneficial effects: I. In operation, through the synergistic action of the storage tank, first metering pump, insulated tank, second metering pump, microreactor body, pressure stabilizing tank, flash tank, and pipeline condenser, an integrated process of precise raw material delivery, microscale reaction enhancement, steady-state pressure control, flash separation, and condensation recovery is achieved. This enables targeted optimized recovery and multi-stage deep purification of hydrogenation products, achieving continuous operation of the entire process from raw material delivery to product separation in anhydride synthesis. Simultaneously, closed-loop recycling of the catalyst is realized, significantly improving the continuity, controllability, and resource utilization efficiency of the process. Through the synergistic action of the first buffer tank, high-pressure diaphragm pump, pipeline explosion-proof preheater, hydrogenation reactor, coil condenser, gas-liquid separator, and second buffer tank, a complete hydrogenation reaction unit is formed, enabling hydrogenation pretreatment processes related to anhydride synthesis and expanding the multifunctionality of the device. The interconnected setup of the gas-liquid separator, second buffer tank, and storage tank allows for the recovery and recycling of unreacted materials, reducing raw material consumption and production costs. Second, the back pressure valve enables precise control of the hydrogenation system's pressure stability, preventing pressure fluctuations from affecting the hydrogenation reaction efficiency and selectivity. It also prevents backflow of high-pressure materials, improving the system's safety and stability. Through the synergistic action of the first and second flow meters, the feed rates of hydrogen and nitrogen can be precisely controlled, meeting the stringent requirements for gas ratios in the hydrogenation reaction. Precise control of the hydrogen-nitrogen ratio allows for flexible adjustment of the reaction system's atmosphere, enabling precise control of the hydrogenation reaction's selectivity and facilitating quality control throughout the production process. Third, the three microreactors connected in series can independently achieve different process steps such as raw material mixing, main reaction, and product purification. Each microreactor can independently optimize reaction conditions (temperature, pressure, residence time, etc.), significantly improving overall reaction efficiency and product purity. Through the coordinated operation of the explosion-proof electrical cabinet, alarm lights, and emergency switches, real-time monitoring of the entire device's operating status is achieved. The alarm lights can promptly sound an alarm in case of abnormalities, and the emergency switch can quickly shut down the system, minimizing safety risks. Attached Figure Description

[0013] Figure 1 This is a three-dimensional schematic diagram of an embodiment.

[0014] Figure 2 This is a breakdown diagram of an embodiment.

[0015] Figure 3 This is a schematic diagram showing the disassembled load-bearing base of an embodiment.

[0016] Figure 4 Examples Figure 2 Enlarged diagram of point A in the middle.

[0017] In the diagram: 1. Storage tank; 2. Load-bearing base; 3. First metering pump; 4. Insulated tank; 5. Second metering pump; 6. Microreactor body; 7. Pressure stabilizing tank; 8. Flash tank; 9. Pipeline condenser; 10. Mounting base; 11. Mounting bracket; 12. Fixed base; 13. First buffer tank; 14. High-pressure diaphragm pump; 15. Pipeline explosion-proof preheater; 16. Hydrogenation reactor; 17. Coil condenser; 18. Gas-liquid separator; 19. Second buffer tank; 20. Back pressure valve; 21. First flow meter; 22. Second flow meter; 23. Explosion-proof electrical cabinet; 24. Alarm light; 25. Emergency switch. Detailed Implementation

[0018] The preferred embodiments of this utility model will now be described in detail with reference to the accompanying drawings.

[0019] like Figures 1-4 As shown, an anhydride synthesis device using a microchannel reactor includes a storage tank 1, which is placed on the top surface of a load-bearing base 2. A first metering pump 3 is fixed on the top surface of the load-bearing base 2, and the storage tank 1 is connected to the input end of the first metering pump 3 through a connecting pipe. A heat preservation tank 4 is placed on the top surface of the load-bearing base 2, and a second metering pump 5 is fixed on the top surface of the load-bearing base 2. The heat preservation tank 4 is connected to the input end of the second metering pump 5 through a connecting pipe. Several microreactor bodies 6 are fixed on the top surface of the load-bearing base 2. A pressure stabilizing tank 7 is placed on the top surface of the load-bearing base 2 and is connected to the microreactor body 6 through a connecting pipe. A flash evaporator 8 is placed on the top surface of the load-bearing base 2 and is connected to the pressure stabilizing tank 7 through a connecting pipe. A pipe-type condenser 9 is fixed on the top surface of the load-bearing base 2 and is connected to the flash evaporator 8 through a connecting pipe. Both the pipe-type condenser 9 and the flash evaporator 8 are connected and fixed with discharge pipes. A mounting base 10 is fixed to the front side of the load-bearing base 2. A mounting frame 11 is fixed to the top surface of the mounting base 10. A fixed base 12 is fixed to the right side of the mounting base 10. A first buffer tank 13 is placed on the top surface of the fixed base 12. Two feed pipes are connected and fixed on the first buffer tank 13. A high-pressure diaphragm pump 14 is connected to the mounting frame 11 by screws. A pipeline explosion-proof preheater 15 is connected to the mounting frame 11 by screws. The output end of the high-pressure diaphragm pump 14 is connected to the input end of the pipeline explosion-proof preheater 15 through a connecting pipe. A hydrogenation reactor 16 is connected to the mounting frame 11 by screws. The first buffer tank 13 is connected to the input end of the hydrogenation reactor 16 through a connecting pipe. The output end of the pipeline explosion-proof preheater 15 is connected to the input end of the hydrogenation reactor 16 through a connecting pipe. A coil-type condenser 17 is placed on the top surface of the fixed base 12. The input end of the coil-type condenser 17 is connected to the output end of the hydrogenation reactor 16 through a connecting pipe. A gas-liquid separator 18 is placed on the top surface of the fixed base 12. The gas-liquid separator 18 is connected to the output end of the coil-type condenser 17 through a connecting pipe. A second buffer tank 19 is placed on the top surface of the fixed base 12. The gas outlet end of the second buffer tank 19 is connected to the input end of the gas-liquid separator 18 through a connecting pipe. The output ends of the gas-liquid separator 18 and the second buffer tank 19 are connected through a three-way pipe. A regulating valve is fixed on the three-way pipe, and the three-way pipe is connected to the storage tank 1.

[0020] In use, the raw material liquid is preheated by the pipeline explosion-proof preheater 15 after being injected by the high-pressure diaphragm pump 14. It is then premixed with hydrogen in the mixer and then enters the hydrogenation reactor 16 together. Under the action of the catalyst bed, the hydrogenation reaction occurs. During the reaction, the reaction temperature is monitored in real time by multi-segment multi-point thermometers to ensure that the reaction conditions are stable and controllable. The product liquid after the hydrogenation reaction and the excess hydrogen enter the coil condenser 17. The gas and liquid are initially separated by condensation. The material from the coil condenser 17 then enters the gas-liquid separator 18. The product liquid is transported to the storage tank 1 through a three-way pipe, while the hydrogen is discharged after passing through the second buffer tank 19. In the subsequent process, the first metering pump 3 and the second metering pump 5 respectively inject the hydrogenated product liquid in the storage tank 1 and the raw material maleic anhydride in the insulation tank 4 into the microreactor body 6 through the connecting pipe. The microreactor body 6 relies on the efficient liquid-liquid mixing characteristics of the microchannel structure to significantly shorten the extraction equilibrium time of the reaction system, while realizing the pressure stability control of the reaction process and the real-time separation and purification of the product, effectively suppressing the occurrence of side reactions and significantly improving the yield of the target product. After the product is discharged from the microreactor body 6, it enters the pressure stabilizing tank 7. The pressure stabilizing tank 7 maintains the system pressure stability through the gas pressure balance mechanism. The material is then transported to flash tank 8 via a connecting pipe. If a low-boiling-point reaction solvent or an excess of low-boiling-point reactants is used in the anhydride synthesis process, these substances will rapidly vaporize into a gas phase after entering flash tank 8 due to the sudden drop in pressure inside the tank. The gas phase is then discharged to pipeline condenser 9 for condensation recovery or harmless treatment. However, as a high-boiling-point organic compound (boiling point is usually above 200℃), anhydride is difficult to vaporize under the reduced pressure environment of flash tank 8 and remains in the tank in liquid form. Finally, it is collected through the liquid phase outlet and discharge pipe of flash tank 8, achieving efficient separation of the target product. Through the synergistic action of storage tank 1, first metering pump 3, insulated tank 4, second metering pump 5, microreactor body 6, pressure stabilizing tank 7, flash tank 8, and pipeline condenser 9, an integrated process of precise raw material delivery, microscale reaction enhancement, pressure steady-state control, flash separation, and condensation recovery is achieved. This enables targeted optimization and multi-stage deep purification of hydrogenation products, achieving continuous operation of the entire process from raw material delivery to product separation in anhydride synthesis. Simultaneously, closed-loop recycling of the catalyst is realized, significantly improving the continuity, controllability, and resource utilization efficiency of the process. Through the synergistic action of first buffer tank 13, high-pressure diaphragm pump 14, pipeline explosion-proof preheater 15, hydrogenation reactor 16, coil condenser 17, gas-liquid separator 18, and second buffer tank 19, a complete hydrogenation reaction unit is formed, enabling hydrogenation pretreatment processes related to anhydride synthesis and expanding the multifunctionality of the device. The interconnection between gas-liquid separator 18, second buffer tank 19, and storage tank 1 allows for the recycling of unreacted materials, reducing raw material consumption and production costs.

[0021] like Figures 1-4 As shown, a back pressure valve 20 is fixed on the connecting pipe at the outlet end of the second buffer tank 19. A first flow meter 21 and a second flow meter 22 are fixed on the two feed pipes of the first buffer tank 13, respectively. The first flow meter 21 is an H2 mass flow meter, and the second flow meter 22 is an N2 mass flow meter. There are three microreactor bodies 6, and the three microreactor bodies 6 are connected in series through connecting pipes. The microreactor bodies 6 are arranged from front to back as follows: first-stage microreactor body 6, second-stage microreactor body 6, and third-stage microreactor body 6. An explosion-proof electrical cabinet 23 is fixed on the top surface of the mounting base 10. An explosion-proof touch screen is fixed on the explosion-proof electrical cabinet 23. An alarm light 24 is fixed on the top surface of the explosion-proof electrical cabinet 23. An emergency switch 25 is installed on the explosion-proof electrical cabinet 23. The explosion-proof electrical cabinet 23, the alarm light 24, and the emergency switch 25 are electrically connected.

[0022] During operation, the back pressure valve 20 precisely controls the pressure stability of the hydrogenation system, preventing pressure fluctuations from affecting the efficiency and selectivity of the hydrogenation reaction, while also preventing backflow of high-pressure materials, thus improving the safety and stability of the system operation. Through the synergistic action of the first flow meter 21 and the second flow meter 22, the feed rates of hydrogen and nitrogen can be precisely controlled, meeting the stringent requirements for gas ratios in the hydrogenation reaction. Precise control of the hydrogen and nitrogen ratio allows for flexible adjustment of the reaction system atmosphere, enabling precise control of the hydrogenation reaction selectivity and facilitating quality control during production. Three microreactor bodies 6 connected in series can respectively realize different process steps such as raw material mixing, main reaction, and product purification. Each microreactor body 6 can independently optimize reaction conditions (temperature, pressure, residence time, etc.), significantly improving overall reaction efficiency and product purity. Through the synergistic action of the explosion-proof electrical cabinet 23, alarm light 24, and emergency switch 25, real-time monitoring of the entire unit's operating status is achieved. The alarm light 24 can promptly issue an alarm in case of abnormalities, and the emergency switch 25 can quickly shut down the system, minimizing safety risks.

[0023] All connecting pipelines are selected according to the characteristics of the materials: PTFE pipes are used for corrosive materials, stainless steel pipes are used for high-temperature materials, a shut-off valve is installed at the outlet of storage tank 1, and a one-way valve is installed between the microreactor bodies 6 to prevent backflow. The microreactor body 6, the heat preservation tank 4, and the second metering pump 5 are connected to the same temperature control system to ensure that the temperature of the material is stable during transportation and reaction. Pressure gauges or sensors are installed at the inlet and outlet of the pressure stabilizing tank 7 and the microreactor body 6 to monitor the pressure in real time.

[0024] The above description is only a preferred embodiment of the present utility model, but the protection scope of the present utility model is not limited thereto. Any equivalent substitutions or changes made by those skilled in the art within the technical scope disclosed in the present utility model, based on the technical solution and the inventive concept of the present utility model, should be included within the protection scope of the present utility model.

Claims

1. An anhydride synthesis apparatus using a microchannel reactor, comprising a storage tank (1) placed on the top surface of a load-bearing base (2), characterized in that, A first metering pump (3) is fixed on the top surface of the load-bearing base (2). The storage tank (1) is connected to the input end of the first metering pump (3) through a connecting pipe. A heat preservation tank (4) is placed on the top surface of the load-bearing base (2). A second metering pump (5) is fixed on the top surface of the load-bearing base (2). The heat preservation tank (4) is connected to the input end of the second metering pump (5) through a connecting pipe. Several microreactor bodies (6) are fixed on the top surface of the load-bearing base (2). A pressure stabilizing tank (7) is placed therein, and the pressure stabilizing tank (7) is connected to the microreactor body (6) through a connecting pipe. A flash tank (8) is placed on the top surface of the load-bearing base (2), and the flash tank (8) is connected to the pressure stabilizing tank (7) through a connecting pipe. A pipe-type condenser (9) is fixed on the top surface of the load-bearing base (2), and the pipe-type condenser (9) is connected to the flash tank (8) through a connecting pipe. Both the pipe-type condenser (9) and the flash tank (8) are connected and fixed with discharge pipes.

2. The anhydride synthesis apparatus using a microchannel reactor according to claim 1, characterized in that: A mounting base (10) is fixed to the front side of the load-bearing base (2). A mounting frame (11) is fixed to the top surface of the mounting base (10). A fixed base (12) is fixed to the right side of the mounting base (10). A first buffer tank (13) is placed on the top surface of the fixed base (12). Two feed pipes are connected and fixed on the first buffer tank (13). A high-pressure diaphragm pump (14) is connected to the mounting frame (11) by screws. A pipeline explosion-proof preheater (15) is connected to the mounting frame (11) by screws. The output end of the high-pressure diaphragm pump (14) is connected to the input end of the pipeline explosion-proof preheater (15) through a connecting pipe. A hydrogenation reactor (16) is connected to the mounting frame (11) by screws. The first buffer tank (13) is connected to the input end of the hydrogenation reactor (16) through a connecting pipe. The pipeline explosion-proof... The output end of the preheater (15) is connected to the input end of the hydrogenation reactor (16) through a connecting pipe. A coil condenser (17) is placed on the top surface of the fixed base (12). The input end of the coil condenser (17) is connected to the output end of the hydrogenation reactor (16) through a connecting pipe. A gas-liquid separator (18) is placed on the top surface of the fixed base (12). The gas-liquid separator (18) is connected to the output end of the coil condenser (17) through a connecting pipe. A second buffer tank (19) is placed on the top surface of the fixed base (12). The gas outlet of the second buffer tank (19) is connected to the input end of the gas-liquid separator (18) through a connecting pipe. The output ends of the gas-liquid separator (18) and the second buffer tank (19) are connected through a three-way pipe. A regulating valve is fixed on the three-way pipe. The three-way pipe is connected to the storage tank (1).

3. The anhydride synthesis apparatus using a microchannel reactor according to claim 2, characterized in that: A back pressure valve (20) is fixed on the connecting pipe at the outlet end of the second buffer tank (19).

4. The anhydride synthesis apparatus using a microchannel reactor according to claim 2, characterized in that: The first buffer tank (13) has a first flow meter (21) and a second flow meter (22) fixed on its two feed pipes respectively. The first flow meter (21) is an H2 mass flow meter and the second flow meter (22) is an N2 mass flow meter.

5. The anhydride synthesis apparatus using a microchannel reactor according to claim 1, characterized in that: The number of microreactor bodies (6) is three, and the three microreactor bodies (6) are connected in series with each other through connecting pipes. The microreactor bodies (6) are arranged from front to back as: primary microreactor body (6), secondary microreactor body (6) and tertiary microreactor body (6).

6. The anhydride synthesis apparatus using a microchannel reactor according to claim 2, characterized in that: An explosion-proof electrical cabinet (23) is fixed on the top surface of the mounting base (10). An explosion-proof touch screen is fixed on the explosion-proof electrical cabinet (23). An alarm light (24) is fixed on the top surface of the explosion-proof electrical cabinet (23). An emergency switch (25) is provided on the explosion-proof electrical cabinet (23). The explosion-proof electrical cabinet (23), the alarm light (24), and the emergency switch (25) are electrically connected.

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